Process for the production of a synthesis gas conversion catalyst

ABSTRACT

A composition for use after reductive activation as a catalyst in the conversion of synthesis gas to hydrocarbons of carbon number greater than one, which composition before reductive activation has the formula: 
     
         Ru.sub.a.A.sub.b.XO.sub.x                                  (I) 
    
     wherein 
     A is an alkali metal, 
     X is a rare earth metal, 
     a is greater than zero and up to 5% w/w, based on the total weight of the composition, 
     b is in the range from zero to 5% w/w, based on the total weight of the composition, 
     x is a number such that the valence requirements of the other elements for oxygen is satisfied, and subject to the requirements of x, X constitutes the remainder of the composition, 
     is produced by the steps of: 
     (A) bringing together at a temperature below 50° C. a rare earth metal oxide, a solution of a soluble salt of ruthenium and a precipitant comprising a carbonate and/or a bicarbonate and/or a hydroxide of an alkali metal or ammonium under conditions whereby ruthenium is precipitated in the form of a heat decomposable compound, 
     (B) recovering the mixture of the rare earth metal oxide and the precipitated ruthenium compound obtained in step A, 
     (C) thermally decomposing thermally decomposable compounds comprised in the mixture recovered in step (B).

This application is a division of application Ser. No. 888,797 filedJuly 23, 1986 now U.S. Pat. No. 4,740,492 issued Apr. 26, 1988.

The present invention relates to a catalyst for use in the conversion ofgaseous mixtures comprising principally carbon monoxide and hydrogen(synthesis gas) to hydrocarbons of carbon number greater than one, inparticular to aliphatic hydrocarbons in the gasoline boiling range, to aprocess for producing the catalyst and to a process utilising thecatalyst in the conversion of synthesis gas to the aforesaidhydrocarbons.

The conversion of synthesis gas to hydrocarbons by the Fishcer-Tropschprocess has been known for many years but the process has only achievedcommercial significance in countries such as South Africa where uniqueeconomic factors prevail. The growing importance of alternative energysources such as coal and natural gas has focussed renewed interest inthe Fischer-Tropsch process as one of the more attractive direct andenvironmentally acceptable routes to high quality transportation fuels.

Of the Group VIII metals, ruthenium has long been known to be one of themost active catalysts in the conversion of synthesis gas, the product,at moderate pressures and above, being high molecular weight paraffinwaxes and, at low pressures, principally methane. Several recent patentpublications, for example U.S. Pat. Nos. 4,042,614; 4,171,320;4,206,134; 4,413,064 and 4,410,637 and GB-A-2,119,277, describe andclaim the formation of different products from synthesis gas usingcatalysts containing ruthenium as an active component.

U.S. Pat. No. 4,042,614 describes a process for the selective synthesisof olefins from C₂ to C₁₀ chain length inclusive from synthesis gasusing as catalyst ruthenium on a titanium-containing oxide support,wherein said titanium-containing oxide support is selected from thegroup consisting of TiO₂, ZrTiO₄, TiO₂ -carbon, TiO₂ -Al₂ O₃, TiO₂-SiO₂, alkaline earth titanates, rare earth titanates and mixturesthereof.

U.S. Pat. No. 4,171,320 describes a process for the synthesis of olefinsof from C₂ to C₅ chain length inclusive from synthesis gas using ascatalyst ruthenium on a support selected from the group consisting of V₂O₃, Nb₂ O₅, Ta₂ O₅, Al₂ O₃ -V₂ O₃, Al₂ O₃ -Nb₂ O₅, Al₂ O₃ -Ta₂ O₅, SiO₂-V₂ O₃, SiO₂ -Nb₂ O₅, SiO₂ -Ta₂ O₅, V₂ O₃ -carbon, Nb₂ O₅ -carbon, Ta₂O₅ -carbon, alkaline earth-group VB oxides, alkali metal-Group VBoxides, Group IVB-Group VB oxides and mixtures thereof.

U.S. Pat. No. 4,206,134 describes a process for the enhanced synthesisof C₂ -C₄ olefins with reduced production of methane from synthesis gasusing as catalyst ruthenium on a manganese-containing oxide support,wherein said manganese-containing oxide support is selected from thegroup consisting of MnO, Al₂ O₃ -MnO, MnO-carbon, Group IVB-manganeseoxide, Group VB-manganese oxides, rare earth-manganese oxides andmixtures thereof.

U.S. Pat. No. 4,413,064 describes a process for the conversion ofsynthesis gas to a product high in straight chain paraffins in thediesel fuel boiling range from synthesis gas utilising a catalystconsisting essentially of cobalt, thoria or lanthana and ruthenium on analumina support wherein said alumina is gamma-alumina, eta-alumina or amixture thereof, said catalyst being prepared by contacting finelydivided alumina with

(A) an aqueous impregnation solution of a cobalt salt, and

(B) a non-aqueous, organic impregnation solution of a ruthenium salt anda salt of thorium or lanthanum.

U.S. Pat. No. 4,410,637 describes a process for the preparation of ahydrocarbon mixture consisting substantially of C₅ -C₁₂ hydrocarbonsfrom synthesis gas using a catalyst containing one or more of iron,nickel, cobalt, chromium and/or ruthenium and, as a carrier, magadite, alaminar crystalline silicate compound capable of absorbing metal ions ormetal salts by intercalation.

Finally, GB-A-2,119,277 describes a catalyst for the selective synthesisof olefins from a mixture of hydrogen and carbon monoxide or hydrogenand carbon dioxide comprising a ruthenium carbonyl compound deposited ona ceric oxide-containing support. In Example 3 there is disclosed acatalyst prepared by impregnating ceric oxide with an aqueous solutionof RuCl₃.3H₂ O (ruthenium content 0.62% w/w). Comparison of theruthenium carbonyl catalyst with the ruthenium-impregnated catalyst forthe conversion of synthesis gas demonstrates that the former catalystproduces considerably less methane and significantly more olefins thanthe latter catalyst.

We have now found that ruthenium-containing catalysts produced byprecipitating the ruthenium component can substantially overcome thedisadvantages in terms of high methane yield and low selectivity toolefins reported for the prior art ruthenium impregnated catalysts.

Accordingly the present invention provides a process for the productionof a composition for use after reductive activation as a catalyst in theconversion of synthesis gas to hydrocarbons of carbon number greaterthan one, which composition before reductive activation has the formula:

    Ru.sub.a.A.sub.b.XO.sub.x                                  (I)

wherein

A is an alkali metal,

X is a rare earth metal,

a is greater than zero and up to 5% w/w, based on the total weight ofthe composition,

b is in the range from zero to 5% w/w, based on the total weight of thecomposition,

x is a number such that the valence requirements of the other elementsfor oxygen is satisfied, and subject to the requirements of x, Xconstitutes the remainder of the composition,

which process comprises the steps of:

(A) bringing together at a temperature below 50° C. a rare earth metaloxide, a solution of a soluble salt of ruthenium and a precipitantcomprising a carbonate and/or a bicarbonate and/or a hydroxide of analkali metal or ammonium under conditions whereby ruthenium isprecipitated in the form of a heat decomposable compound,

(B) recovering the mixture of the rare earth metal oxide and theprecipitated ruthenium compound obtained in step A,

(C) thermally decomposing thermally decomposable compounds comprised inthe mixture recovered in step (B).

For the purpose of the present invention rare earth metals are definedas metals having atomic numbers of from 57 to 71 inclusive. A preferredrare earth metal oxide is ceria (CeO₂) which may be in a substantiallypure form or may be in the form of a mixture with other rare earth metaloxides, in which form it may be obtained commercially.

In the composition of formula (I) A is an alkali metal, which largelyfor reasons of availability and cost, is preferably either sodium orpotassium. X as mentioned hereinbefore is preferably cerium. Preferablythe amount (b) of alkali metal is less than 2% w/w, even more preferablyless than 1% w/w. a in the formula (I) is preferably less than 1% w/w.

As regards step (A) of the process, the rare earth metal oxide maysuitably be brought together with an aqueous solution of a water solublesalt of ruthenium, in which solution the rare earth metal oxide issubstantially insoluble. Suitably an aqueous solution of the precipitantmay be added to an aqueous solution of the ruthenium salt containingalso the rare earth metal oxide, though other variants of the order ofaddition will be readily apparent to those skilled in the art and may beused if desired. Whilst any soluble salt of ruthenium may be employed,it will usually be found convenient to use ruthenium in the form of thechloride because this is a commercially available form.

The precipitant may be a carbonate and/or a bicarbonate and/or ahydroxide of an alkali metal, which is preferably either sodium orpotassium. Instead of using a pre-formed carbonate or bicarbonate it ispossible to use the precursors of these salts, for example a watersoluble salt and carbon dioxide. In any event, b in the aforesaidformula (I) will have a value greater than zero, which value may beadjusted if desired by washing or addition of further alkali metalcompound. Alternatively, ammonium carbonate and/or bicarbonate and/orhydroxide may be employed as the precipitant, in which case the value ofb in the catalyst as initially produced will be zero, though this valuemay subsequently be adjusted if desired by addition of alkali metal.

The precipitation is preferably carried out at a temperature below 30°C. It will usually be found convenient to operate at room temperature,for example 15° to 25° C. Catalysts produced at low temperatures aregenerally more active than similar catalysts wherein the ruthenium isprecipitated at high, for example, 80°-90° C., temperatures.

Addition of the precipitant to the solution of the ruthenium salt causesthe initially low pH of the mixture to rise. It is desirable in thepreparation of catalysts according to the invention that the final pH ofthe mixture is greater than 6, preferably in the range from 6 to 10,even more preferably in the range from 8 to 10. The precipitant may beadded until a pH in the aforesaid range is achieved, whereupon theaddition of further precipitant may be discontinued, thereby arrestingthe rise in the pH. In order to improve the homogeneity of the catalystit is preferred to agitate the mixture during precipitation, suitably bymechanical stirring. After precipitation, it is preferred to maintainthe mixture at a temperaure close to boiling for a period of at least 15minutes, preferably whilst stirring, for the purpose of completing theprecipitation.

The amounts of the reagents employed should be such as to satisfy thestoichiometric relationships in the formula (I).

In step (B) of the process of the invention the precipitate obtained instep (A) is recovered. This may suitably be accomplished by filtrationbut other methods for separating solids from liquids, for examplecentrifugation, may be employed. After recovery it is preferred to washthe precipitate, suitably with water, so as to remove unwanted residualsoluble matter. It is also preferred to dry the precipitate, suitably atan elevated temperature below 150° C., for example about 120° C.

In step (C) of the process thermally decomposable compounds comprised inthe mixture obtained in step (B) are thermally decomposed. This maysuitably be achieved by heating the mixture, suitably in a non-reducingatmosphere, for example a stream of inert gas, such as nitrogen, or anoxygen-containing gas, such as air, at a temperature suitably in therange from 250° to 600° C.

Before use as a catalyst in the production of hydrocarbons fromsynthesis gas it is necessary for the composition of formula (I) to bereductively activated. Reductive activation may be accomplished bycontacting the composition at elevated temperature with a reducing gas,for example hydrogen which may be diluted with an inert gas such asnitrogen. Typically, the conditions employed may suitably be a pressurein the range from 1 to 100 bar and a temperature in the range from 150°to 300° C., suitably for a period of up to 24 hours or longer. Whilst itis preferred to effect the reductive activation step as a discrete stepprior to use as a catalyst for the conversion of synthesis gas, it maybe incorporated into the synthesis gas conversion process and effected`in situ`.

It will be appreciated by those skilled in the art that under certaincircumstances the thermal decomposition step [step B] and the reductiveactivation may be accomplished in one and the same operation, therbysimplifying the process.

The present invention also provides a process for the production ofhydrocarbons having a carbon number greater than one from synthesis gaswhich process comprises contacting synthesis gas with the reductivelyactivated composition of formula (I) at a temperature in the range from190° to 400° C. and a pressure in the range from 0 to 100 bar.

As is well known in the art synthesis gas principally comprises carbonmonoxide and hydrogen and possibly also minor amounts of carbon dioxide,nitrogen and other inert gases depending upon its origin and degree ofpurity. Methods for preparing synthesis gas are established in the artand usually involve the partial oxidation of a carbonaceous substance,e.g. coal. Alternatively, synthesis gas may be prepared, for example bythe catalytic steam reforming of methane. For the purpose of the presentinvention the carbon monoxide to hydrogen ratio may suitably be in therange from 2:1 to 1:6. Whilst the ratio of the carbon monoxide tohydrogen in the synthesis gas produced by the aforesaid processes maydiffer from these ranges, it may be altered appropriately by theaddition of either carbon monoxide or hydrogen, or may be adjusted bythe so-called shift reaction well known to those skilled in the art.

The temperature is preferably in the range from 250° to 350° C. and thepressure is preferably in the range from 10 to 50 bar. The GHSV maysuitably be in the range from 100 to 5000 h⁻¹.

The process may be carried out batchwise or continuously in a fixed bed,fluidised bed or slurry phase reactor.

In a modification of the process for the production of hydrocarbons,there may be combined with the catalyst an inert material, for examplesilica. It is preferred, however, to combine the catalyst with azeolite.

The zeolite may be either physically admixed with the composition toform an intimately mixed bed or may be separate therefrom, for examplein the form of a split bed, the zeolite forming one portion of the bedand the catalyst another. In the case of a physical admixture, thezeolite may be mixed with the composition either before or afterreductive activation. Alternatively, the precipitation (step A) in theprocess for producing the composition of formula (I) may be performed inthe presence of the zeolite, particularly when the precipitant isammonium carbonate and/or bicarbonate and/or hydroxide.

A suitable zeolite is an MFI-type zeolite, for example ZSM-5 asdescribed in U.S. Pat. No. 3,702,886. It is preferred to use thehydrogen form of the zeolite which may be obtained by acid exchange orby thermal decomposition of the ammonium-exchanged form of the zeolite.Preferably the alkali metal-free composition (b in the formula (I)=0) ismodified by combination with the zeolite. Suitably the ratio of thenumber of parts by volume of catalyst composition to the number of partsby volume of the zeolite may be in the range from 5:1 to 1:5, preferablyabout 2:1. Combination with a zeolite can improve the selectivity togasoline range paraffinic hydrocarbons.

DETAILED DESCRIPTION OF INVENTION

The invention will now be further illustrated by the following Examples.In all the synthesis gas conversion reactions there was employed thesame slurry phase reactor using fine particles of the catalyst suspendedin a hydrocarbon wax.

CATALYST PREPARATION EXAMPLE 1 Catalyst A (0.5% w/w Ru on ceria)

Cerium oxide (CeO₂, 60 g; 0.349 mol) was added to a 500 ml solution ofruthenium chloride (RuCl₃.2H₂ O, 0.72 g; 0.003 mol) and stirredvigorously for one hour. To this a 50 ml solution of sodium carbonate(Na₂ CO₃.10H₂ O, 2.55 g; 0.009 mol) was added at room temperature (about20° C.) dropwise over 30 minutes. After a further hour the solution washeated to boiling to ensure complete hydrolysis of the rutheniumchloride. After holding for 30 minutes a solution of sodium formate(NaHCO, 0.95 g; 0.018 mol) in 50 mls water was added over 30 minutes tothe boiling solution. After a further hour the catalyst slurry wasallowed to cool, was filtered and extremely thoroughly washed withwater. After drying in an oven for 16 hours at 125° C., the catalyst wasactivated under a steady stream of hydrogen for 16 hours at 270° C.before testing.

EXAMPLE 2 Catalyst B (0.5% w/w Ru on ceria)

Cerium oxide (CeO₂, 40 g; 0.233 mol) was added to a 500 ml soluton ofruthenium chloride (RuCl₃.2H₂ O, 0.48 g; 0.002 mol) and vigorouslystirred for 30 minutes. To this ammonium carbonate (NH₄ HCO₃.NH₂ COOHN₄,1.5 g: 0.010 mol) dissolved in 50 mls water was added at roomtemperature (about 20° C.) dropwise over a further 30 minutes. Theslurry was then cold stirred for one hour, before heating to boiling fora further one hour to ensure complete ruthenium chloride hydrolysis. Themixture was then allowed to cool, filtered and was thoroughly washedbefore drying in an oven at 125° C. for 16 hours.

This catalyst was activated under hydrogen as in Example 1.

EXAMPLE 3 Catalyst C (0.5% w/w Ru on ceria)

Cerium oxide (CeO₂, 40 g; 0.233 mol) was placed in an evaporating basinheated on a steam bath. Ruthenium chloride (RuCl₃.2H₂ O, 0.48 g; 0.002mol) dissolved in 50 mls water was slowly added, stirring the mixturecontinuously as the water dried off. After complete addition thecatalyst cake was dried at 125° C. for 8 hours in an oven.

The catalyst was activated as in Example 1.

EXAMPLE 4 Catalyst D (0.5%, w/w Ru on ceria)

Cerium oxide (CeO₂, 40 g; 0.233 mol) was added to a 500 ml solution ofruthenium chloride (RuCl₃.2H₂ O, 0.48 g; 0.002 mol) and stirred for 30minutes. The mixture was then heated to boiling. Ammonium carbonate (NH₄HCO₃.NH₂ COONH₄, 1.5 g; 0.010 mol) dissolved in 50 ml water was addeddropwise over a further 30 minutes. After 1 hour of slurrying themixture was allowed to cool, was filtered and thoroughly washed. Thecatalyst was then dried for 16 hours at 125° C., before activation inthe same way as Example 1.

CATALYST TESTING EXAMPLE 5

The Catalyst (A) of Example 1 was tested for the conversion of synthesisgas to hydrocarbons in a slurry phase reactor under the followingconditions:

CO:H₂ (molar ratio)=1:2

Pressure=20 bars

Temperature=290° C.

GHSV (based on wax)=268 h⁻¹

The results are given in the Table.

EXAMPLE 6

Example 5 was repeated except that the Catalyst (B) of Example 2 wasused in place of Catalyst (A).

EXAMPLE 7

Example 5 was repeated except that the Catalyst (C) of Example 3 wasused in place of Catalyst A.

EXAMPLE 8

Example 5 was repeated except that the Catalyst (D) of Example 4 wasused in place of Catalyst (A).

The results of Examples 6 to 8 are given in the Table.

                  TABLE                                                           ______________________________________                                                        Molar Selectivity (%)                                         Example                                                                              Catalyst Conversion                                                                              CO.sub.2                                                                           CH.sub.4                                                                           C.sub.5.sup.+ hydrocarbons                ______________________________________                                        5      A        30        2.7  14.7 46.5                                      6      B        36        2.2  13.5 46.6                                      7      C        36        0.85 25.6 38.8                                      8      D         8        2.7  17.2 38.8                                      ______________________________________                                    

We claim:
 1. A process for the production of hydrocarbons having acarbon number greater than one from synthesis gas which processcomprises contacting synthesis gas with a catalyst at a temperature inthe range from 190° to 400° C. and a pressure in the range from 0 to 100bar,said catalyst comprising a reductively activated composition, whichcomposition before reductive activation has the formula:

    Ru.sub.a A.sub.b XO.sub.x                                  (I)

wherein A is an alkali metal, X is a rare earth metal, a is greater thanzero and up to 5% w/w, based on the total weight of the composition, bis in the range from zero to 5% w/w based on the total weight of thecomposition, x is a number such that the valence requirements of theother elements for oxygen is satisfied, and subject to the requirementsof x, X constitutes the remainder of the composition.
 2. A processaccording to claim 1 wherein the temperaure is in the range from 250° to350° C. and the pressure is in the range from 10 to 50 bar.
 3. A processaccording to claim 1 wherein the catalyst is in a slurry phase.
 4. Aprocess according to claim 1 wherein the reductively activatedcomposition of formula (I) is combined with a zeolite.
 5. A processaccording to claim 4 wherein the zeolite is ZSM-5 in the hydrogen form.